Production of organic fluorine compounds



June 18, 1935. H. w. DAUDT ET AL 2,005,709

PRODUCTION OF ORGANIC FLUORINE COMPOUNDS Filed Oct. '7, 1953 2 Sheets-Sheet 1 GO Q sr----" INVENTORS Herber UZDaudc BY moriimerfl. 0 km" A TTORNE Y.

June 18, 1935. H. w. DAUDT El AL 2,005,709

PRODUCTION OF ORGANIC FLUORINE COMPOUNDS Filed 00x7, 1933 2 Sheets-Sheet 2 Hum M Her-Ber UlDaucH INVENTORS 1 mor timerfl. ouker D 1 A TTORNEY.

Patented June 18, 1935 PRODUCTION OF ORGANIC FLUORINE COMPOUNDS Herbert Wilkens Daudt and Mortimer Alexander Youker, Wilmington, Del., assignors to Kinetic Chemicals, Inc., Wilmington, Del., :1. corporation of Delaware Application October 7,

11 Claims.

This invention relates to organic fluorine compounds, more particularly fluorinated acyclic hydrocarbons, and a process for the production thereof.

This application is a continuation-in-part of our co-pending U. S. application Serial No. 483,- 289, filed September 20, 1930.

Halogen atoms other than fluorine, i. e., chlorine, bromine and iodine, attached to acyclic carbon atoms, may be replaced by fluorine by reaction with various fluorinating agents. Fluorination is sometimes effected in the presence of antimony halides. Antimony halides, particularly pentavalent antimony halides, are normally somewhat volatilized under the conditions of reaction and contaminate gaseous reaction products. Such contamination causes difliculty in purifying the gaseous reaction products which are removed from the reaction zone, particularly on account of the formation of plugs in the lines. Further, if the volatilized antimony halide is not recovered, it represents large economic loss.

Ordinarily, in fiuorination processes of the type described,-reaction products of varying fluorine content are formed. In addition, the gases from the reaction zone normally contain hydrogen halides and some unconverted raw material. Where it is desired to produce only a single product, as, for example, difiuoro-dichloro methane.

or tetrafiuoro-dichloro ethane, it is undesirable to subject all of the reaction products to purification.

It' is an object of the present-invention to provide a new and improved process for the production of fluorinated acyclic hydrocarbons. A further object is to provide an improvement in fluorination' processes of the character described whereby the catalyst volatilized by the reaction is recovered efiiciently. Another object is to provide an improvement in fluorination processes of the character described whereby low boiling products may be recovered directly substantially free from higher boiling p u s. A Still further object is the provision of an improvement in the production of vaporizable fluorinated compounds by fluorinating liquid halogenated acyclic hydrocarbons in the presence of an antimony fluorinating catalyst, characterized by the fact that the handling of excessive amounts of material in the purifying, condensing and final distillation of the product is avoided. A more specific object is the provision of an improved process for producing difiuoro-dichloro methane. Other objects will appear hereinafter.

These objects are accomplished according to 1933, Serial No. 692,696

the present invention whereby in a fiuorination process involving the use of an appreciably volatile fiuorinating catalyst, such as antimony halide, and removal from the reaction zone of evolved vapors containing fluorinated compounds, as well as vother substances such as, for example, volatilized catalyst and imconverted reactants, the process is characterized by the improvement that the evolved vapors are passed through at least two baths of a substance which may be fluorinated and which has a solvent, action on the fluorinating catalyst, said baths being maintained at different temperatures. Portions of the baths or scrubbing liquids, as they are commonly called, may be introduced into the fluorination reaction zone intermittently or continuously, thereby returning volatilized catalyst and incompletely fluorinated compounds. The process may be so operated that all of the compound to be fluorinated is introduced into the reaction zone countercurrent to the issuing gases, that is, after first being used as a scrubbing liquid.

In the drawings:

Figure 1 represents one form of apparatus for carrying out the process of invention, characterized by circulation of the scrubbing liquids.

Figure 2 represents another form of apparatus for carrying out the process of the invention in which the scrubbers are non-circulating.

The apparatus in each figure comprises generally a reactor D into which the fluorinating agent and compound to be fluorinated may be introduced directly from storage vessels A and B, respectively. The vapors from reactor D are treated in a scrubber E under such conditions that volatilized catalyst is efliciently removed from the gas stream. The scrubbing liquid is the compound to be fluorinated. This is introduced into scrubber E from storage vessel B and, after being used in scrubbing the reaction gases, is passed from scrubber E into reactor D (in Fig. 1 by way of a calibrated reservoir of weigh tank G).

The vapors passing through the scrubbing liquid in E are treated with a second scrubbing liquid in F. This scrubbing liquid is also a compound to be fluorinated, but the physical conditions maintained in scrubber F are different from those maintained in scrubber E. The scrubbing liquid in F is maintained at a temperature sufficiently low to condense most of the higher boiling incompletely fluorinated products in the gas stream. The temperature at which these products may be so completely condensed does not normally promote the efllcient removal of antim'ony catalyst from the gas stream. The

scrubbing liquid from scrubber F is also introduced into the reaction zone for fiuorination. In the apparatus of Fig. 1 this is effected by first passing the scrubbing liquid from scrubber F into a calibrated reservoir H and then to reactor D. v

The gases passing through scrubber F may be conveniently purified in the manner desired. This purification generally includes: (1) a chemical treatment to remove hydrogen halides, for example, by scrubbing with water and/or aqueous solutions of sodium hydroxide, potassium hydroxide, milk of lime or the like; (2) a chemical treatment to remove .water vapor, e. g., by treatment with concentrated suliuric acid, stick caustic or other suitable dehydrating substance. The resultant dry, neutral vapors may be condensed and the fiuorinated organic compoundor compounds separated by fractional distillation of the condensate, or in any other suitable manner. The treatment of the reaction gases in the second scrubber F is normally suflicient to separate almost all of the unconverted raw material as well as high proportions of the higher boiling fluorinated compounds; but where these substances are present in the final condensate, they may be used again in the process, e. g., by direct introduction into the reaction zone in reactor D or by introduction into scrubbers E or F.

The invention will be more fully understood by reference to the following detailed description. For convenience, the process is described in connection with specific substances, namely, hydrogen fluoride (the fiuorinating agent), carbon tetrachloride (the compound to be fluorinated) and an' antimony fluorochloride (the catalyst).

With reference to Figure 1, the reactor D, as illustrated, is provided with a stirring or agitating device 2 operated by a suitable mechanical means, such as a motor (notshown). A jacket 3,

having an inlet 4 and an outlet 5 for a heat'transfer medium, is provided to maintain the desired reaction temperature. A bottom valved outlet 6 is provided to remove the contents'of the reactor D.

In practising the invention, the antimony halide catalyst is charged into the reactor and heated to the desired reaction temperature bypassing a heating fluid, for example, steam, into the jacket 3, as indicated. When the desired reaction temperature has been attained (say 45 C. to 0.), gaseous hydrogen fluoride from storage vessel A is introduced into reactor D through line 1 and valve 8. Simultaneously, carbon tetrachloride isintroduced into reactor D from storage vessel B through line 9 and valve i0.

As a result of the reaction, the carbon tetrachloride has a part of its chlorine replaced by fluorine. The reaction normally produces some of each of the compounds CClsF and CC12F2. The proportions of these substances will depend upon the specific operating conditions. The reaction also produces hydrogen chloride. By a proper regulation of the temperature of the reaction, the time of the reaction or contact of the materials, relative proportions of the ingredients, pressures, etc., the production of the desired compounds is maintained at a maximum.

The reaction gases containing substances of the type enumerated and some unconverted hydrogen fluoride and carbon tetrachloride pass through line H and valve l2 into scrubber E.

Scrubber E, as illustrated in the drawings, is of the circulating type, comprising a column l3, into. which the gases in line II are introduced. and a reservoir for the scrubbing liquid l4. Reservoir I4 is provided with a jacket I! having an inlet l6 and an outlet l1 for a heattrans'fer medium. A suitable agitating device, such as illustrated at l8, operated by a motor (not shown) or by any other convenient method, facilitates contact of the scrubbing liquid with the reaction gases and also serves to prevent clogging of the lines by solid particles which may be removed from the gas stream. The liquid in reservoir I4 is re-circulated through tower IS in countercurrent flow with the reaction gases from line ll. Re-circulation is effected by way of valve l9,

line 20, pump 2|, line 22, valve 23 and line 24.

Fresh scrubbing liquid is added to the system from storage vessel B by way of line 25 and valve 26. The temperature of the scrubbing liquid in scrubber E is maintained relatively high in order to remove antimony halides from the reaction gases. In addition to the removal of antimony halides, scrubber E also removes some of the unconverted carbon tetrachloride from the gas stream. In general, the temperatures preferably employed are too high to effect removal of the desired proportions of the higher boiling fluorinated products.

The scrubbing liquid contained in scrubber E, when continuous operation is established, is introduced into reactor D. This returns the antimony catalyst to the reaction zone. The introduction of the scrubbing liquid into reactor D from scrubber E is effected by passing it through line 21, controlled by valve 28, into a calibrated reservoir G and then through line 29, valve 30 and line 3|, in the order named. Vessel G is provided with a valved bottom outlet 32 and an agitator 33. The proportions of .the scrubbing liquid introduced into reactor D from vessel G are preferably regulated according to the rate of introduction of hydrogen fluoride into reactor D and the rate of fiuorination. As the scrubbing liquid is withdrawn from scrubber G fresh carbon tetrachloride from storage vessel B is introduced into scrubber E through line 25 controlled by valve 26.

The exit gases from the top of column iii of scrubber E enter line 34 controlled by valve 35 and are thereby introduced into the second scrubber illustrated at F. Scrubber F is similar in construction to scrubber E comprising a column 36 into which the gases from line 34 are introduced and a reservoir 31 for the scrubbing liquid. Reservoir 31 is provided with a jacket 38 having an inlet- 39 and an outlet 40 for a heat transfer medium. An agitating device 4| is also provided. The scrubbing liquid which may be fluoro-trichloro methane, carbon tetrachloride or both, is introduced into scrubber F from storage vessel 0 through line 42 and valve 43. The scrubbing liquid is re-circulated from reservoir 31 to column 36 by way of line 44, valve 45, pump 46, line 41, valve 48 and line 49. The temperature maintained in scrubber F is normally relatively low in comparison to the temperature of scrubber E. At the relatively low temperatures employed in scrubber F, higher boiling fiuorinated products and unconverted carbon tetrachloride are removed from the gas stream.

At intervals or continuously, the liquid in reservoir 31 is introduced into a calibrated reservoir or weigh tank H through line 50 and valve 5|. At the same time, fresh scrubbing liquid is added from storage vessel C. As the fluoridation in reactor D progresses the liquid in reservoir H is added thereto in regulated proportions through .line 3I', controlled by valve 52. Reservoir H is provided with a valved bottom outlet 53 for drain: age and an agitator 59. When continuous operation has been established, valve I is preferably kept closed and most of the carbon tetrachloride or fiuoro-trichloro methane to be fluorinated is preferably introduced from G or H or both into the reaction zone after first being contacted with the reaction gases inscrubbers E and F.

The gases which pass through scrubber F are removed through line 54, controlled by valve 55, and may be further purified in any suitable manner, for example, by passing them through a dilute solution of sodiu hydroxide and then concentrated sulfuric acid, as previously described.

In carrying out the process of the invention, it will be recognized that various modifications may be made in the exact method of procedure. Thus, the calibrated reservoirs or weigh tanks G and H may be omitted from the construction of the apparatus, or the process may be operand F, is highly desirable inorder to prevent stoppage by the presence of suspended materials. Such stoppages may cause considerable annoyance because of the attending interruptions in operation and the handling oficorrosive and toxic materials. Whilenot show ns as such, lines 1, 9 and SI are preferably standpipes, that is, pipes extending to the bottomof the reactor D. Columns I3 and 36 are preferably packed with some inert material such as that used in the construction of the equipmentQ The lines I I and 34 which deliver the gases to be purified to columns I3 and 36, respectively, preferably enter the columns near the bottom, for instance, at points about one-third of the distance from the bottom to the top of each column. The columns are shown with parts broken away in order to facilitate the drawings. The storage vessels A, B, and C may be filled through valved inlets 56, 51 and 58.

When the process of the invention is carried out in an apparatus such as described in Fig. 2,

with the description of Fig. 1.

the hydrogen fluoride (the fiuorinating agent) is introduced into reactor D from reservoir A through line I02 and valve I04. Carbon tetrachloride (the compound to be fiuorinated) is introduced into the system from vessel B through lines I06 and H0 controlled by valves I08 and H2, respectively. An agitator H4 is provided in reactor D.

The reaction gases pass upwards through line II 6 controlled by valve II8, through lines I20 and I22 into scrubber E. After passing through the scrubbing liquid in E, they enter line I24 and pass to scrubber F. The gases passing through the scrubbing liquid in F are withdrawn through line I26 controlled by valve I28. I

The compositions of the scrubbing liquids in E and F may be similar to those given in connection Scrubbing liquid for. scrubber F may be introduced from reservoir C through line I30 controlled by valve I32. Suitable liquid level indicating devices I34 and I36 are provided on scrubbers E and F, respectively.

As the fiuorination reaction in reactor D proceeds, the scrubbing liquids from E and F are introduced into reactor D aeither continuously or intermittently, the introduction being made through lines I38 and/or I40. Line I38 is provided with a valve I38 while line I40 is provided with a valve MI. The liquid in scrubber E may be introduced into line I38 through line I42 controlled by valve I44 or overflow 1ine,,l46 controlled by valve I48. Line I46 connects also with line I40.

Portions of the apparatus which come into contact with hydrogen halides during the process have usually been constructed ofor lined with some corrosion-resistant material such as copper. Monel metal, lead, steel, chromium steels and iron.

The invention will be further understood, particularly as regards proportions of materials, temperatures and pressures, from a consideration of the following examples, in which the parts are by weight. g

Example I g A mixture of '75 parts of antimony pentachloride, 10 parts of antimony trichloride and 10 parts of chloroform, was placed in the reactor of a set-up similar in principle to that illustrated in Fig. 2 of the drawings. The temperature of the mixture was maintained at about 75 C., and substantially anhydrous hydrogen fluoride and chloroform were added to the reaction zone at the rate of about 10 parts of hydrogen fluoride per hour and 70 parts of chloroform per hour. The introduction of chloroform was effected by first introducing it into scrubbers E and F. The first scrubber E was maintained at a temperature of about 30 C. to about C. and the second scrubber F was maintained at a temperature of about 10 C. to about 15 C. The'reaction gases, after passing through scrubbers E and.F, were successively scrubbed with dilute solutions of 40 sodium hydroxide and concentrated sulfuric acid in the order named. The sodium hydroxide and sulfuric acid scrubbers were operated at a temperature of about 25 C. The product, condensed at about -50 0., consisted of a mixture of difiuoro-chloro-methane and fluoro-dichloro-methane which contained a smallamount of unconsumed chloroform. When a sample portion of the vapors from E were purified from the acids, dried and then condensed, the product was found to contain much greater proportions of CHCla and of CHFClz and smaller proportions of CHFzCl than the above product. The yield of fiuorinatedproduct was about 80% to 85%. The various components of the condensate were separated by fractional distillation. Difiuoro-chloro-methane boils at about -4l C., and fiuoro-dichloro-methane at about 8.7 C., under atmospheric pressure.

Example II Five hundred parts of gaseous, substantially dry, hydrogen fluoride were passed rapidly and steadily into a reactor, such as illustrated at D in Fig. 1 of the drawings,- over a period of twentyfive hours. The reactor contained 600 parts of antimony pentachloride which was maintained at a temperature of about 60 C. During this time 1925 parts of carbon tetrachloride were run into the reactor D from reservoirs B and C by the way of scrubbers E and F and weigh tanks G and H. The carbon tetrachloride in scrubber E was maintained at a temperature of about +30 C. and the second scrubbing liquid, contained in scrubber F, was maintained ata temperature of about -10 C. The reaction gases, after passing through scrubber F, were passed successively through caustic and sulfuric acid scrubbers operated at a temperature of about 25 C. to about 30 C. The product was then condensed.

The yield of fluorinated products was about 90% to about 95%. The condensate boiled at about C. and comprised substantially 75% difluoro-dichloro methane and fluoro-tri- 'chloro methane. Only small amounts of carbon tetrachloride were present. No stoppages in the return lines from the scrubbers were encountered.

Example III An apparatus similar in principle to that described in Fig. 1 of the drawings was used. Reactor D was charged with approximately 300 parts of an antimony fluoro-chloride catalyst, having a fluorine content of about 6% to about 7%, and hydrogen fluoride was introduced into.

reactor D at the rate of about 8.75 parts per hour. Scrubbing liquid comprising substantially carbon tetrachloride was simultaneously introduced into D from weigh tanks G and H at the rate of about 38.2 parts per hour.

When the supply of the scrubbing liquid in G and H was nearly exhausted, the feed of this material to reactor D was temporarily interrupted.

while vessels G and H were being refilled with scrubbing liquid from'scrubbers E and F. Subsequently, while the scrubbing liquid was being introduced into the catalyst at the rate of 382 parts per hour, fresh carbon tetrachloride was introduced into scrubbers E and F from storage vessels B and C at the same rate.

The temperature of scrubber E was maintained at about C. and the temperature of scrubber F at about -10 C. The vapors passing through scrubber F were further purified by treatment. with an aqueous solution of sodium hydroxide and concentrated sulfuric acid at temperatures of about 25 C. to about 30 C.. and the resultant product was condensed. The composition of the product was essentially the same as the product of Example II. Difluoro-dichloro methane was recovered in good yield.

Example IV An apparatus similar to that described with reference to Fig. 1 of the drawings was used. About 880 parts of anhydrous antimony trichloride were charged into reactor D and treated with liquid chlorine at a temperature of about 100 C.

and a pressure of about 100 pounds per square inch (gauge) until approximately 142 parts of chlorine, had been added. Liquid hydrogen fluowith chlorine, were then introduced into the catalyst at the following hourly rates;

Parts Hydrogen fluoride 3.0 Chlorine 2.5 Perchloro-ethylene 5.9

The gases from the reaction zone were introduced into scrubber E which was maintained at a temperature of about 90 C. to about 100 C. The scrubbing liquid in scrubber E was initially perchloro-ethylene from storage vessel B.

The gases from scrubber E passed to scrubber F which was maintained at a temperature of about 10C. to about 15 C. The scrubbing liquid in scrubber F was initially perchloro-ethylene.

In the early stages of operation the fluorinated product in the reaction gases was largely trifluoro-trichloro-ethane, most of which condensed in scrubber F. Unconverted perchloro-ethylene in the reaction gases was removed in both scrubbers E and F. The relatively high temperature maintained in scrubber E enabled the eflicient removal of substantially all of the volatilized antimony compounds in the reaction gases.

As the reaction proceeded, the direct introduction of perchloro-ethylene from reservoir B was discontinued and instead the scrubbing liquids from scrubbers E and F were introduced into the reaction zone through the weigh tanks G and H. As the scrubbing liquids were exhausted, they were replenished with perchloro-ethylene and trifluoro-trichloroethane. The amount of these liquids introduced into the catalyst was gradually increased up to about to parts per hour. Tetrafluoro-dichloro-ethane was formed in increasing quantities until the rate of production finally reached about 4 parts per hour.

The gases which passed through scrubber F were further purified by scrubbing with water, a dilute solute of sodium hydroxide and concentrated sulfuric acid in the order named at temperatures of about 50 C. to about C. The resultant product was condensed and the condensate fractionated. Approximately. 33 parts of trifiuoro-trichloro-ethane were produced with every 100 parts of tetrafiuoro-dichloro-ethane.

The trifluoro-trichloro-ethane was returned to the reaction zone, being introduced into scrubber F by way of reservoir C. After continuous operation had been established, the hourly introduction of raw materials into the system was:

Parts Chlorine 2.0 Perchloro-ethylene 4.75 Hydrogen fluoride 2.5 Trifluoro-trichloro-ethane 1.25

It will be understood that the invention is not limited by the foregoing examples. In general, it is applicable to the treatment of reaction gases containing fluorinated acyclic hydrocarbons prepared by a fluorination reaction involving the use of a volatile catalyst, such as an antimony halide. The fluorinating agent may be hydrogen fluoride or any other volatile fluorinating agent which is effective in the presence of a catalyst.

The compounds which are used as scrubbing liquids for the reaction gases and which are subsequently fluorinated in accordance with the invention are preferably liquid acyclic halogen compounds containing at least one halogen atom other than fluorine. Included among such compounds may be mentioned carbon tetrachloride, chloroform, tetrachloro-ethane, perchloro-ethylene, fluoro-trichloro-methane,trifluoro-trichloro-ethane, trichloro-ethylene, tribrom-ethane and the like. Where the acyclic halogen compound to be fluorinated is a solid under the conditions of scrubbing, it may be dissolved in a suitable solvent, which is inert under the conditions of reaction, or may be further fluorinated. Thus, hexachloroethane may be used as a scrubbing liquid under I 5 ably an antimony halide containing a composi 5 Where super-atmospheric pressures are used, itv

tion represented empirically by SbFzHBJB-z in which Hal represents a halogen other than fluorine, and :c'represents a positive value less than 5. Especially desirable results have been obtained in the application of the invention to the production of fluorochloro acyclic hydrocarbon derivatives by the fluorination of chlorinated acyclic hydrocarbon derivatives with hydrogen fluoride inthe presence of an antimony fluorochloride. The antimony catalyst is preferably a mixture of pentavalent and trivalent antimony halides. In general, the presence of antimony trihalides' is advantageous in preventing dissociation of the catalyst.

- As indicated by Example IV, a free halogen may be present or may be added to the reaction zone during the fluorination. It will be recognized that the free halogen used should correspond to the type of product desired; that is, in the production of fluoro-chloro acyclic hydrocarbon derivatives, chlorine may be added to the reaction zone, while in the production of fluorobromo acyclic hydrocarbon derivatives, bromine may be added to the reaction zone.

The temperature of the scrubbing liquid employed to remove volatile catalyst from the reaction gases issubject to some variation, depending largely upon the specific compound being fiuorinated and the products derived therefrom. Generally speaking, the conditions of temperature and pressure for the removal of volatilized antimony catalyst should be so regulated that the scrubber liquid is maintained in liquid form and that it readily dissolves antimony halides. Where the scrubber liquid is chloroform, or carbon tetrachloride, temperatures within the range of about 25 C. to 45 C. are preferably used.

is desirable to maintain higher temperatures in this step of the process. Higher temperatures may also be maintained where higher boiling acyclic halogen derivatives are fiuorinated. Thus, in the fluorination of compounds suchas hexachloroethane, tetrachloro ethane and trichloro ethylene, good results have been obtained in the removal of antimony catalyst from the gas stream under pressure by scrubbing with these acyclic halogen compounds at temperatures within the range of about 90 C. to about 100 C. (cf. Example IV).

The temperature of the scrubber liquid which is primarily used to remove unconverted organic raw materials and higher boiling fiuorinated compounds from the reaction gases may vary within relatively wide limits, depending largely uponthe boiling points of these compounds under the specific conditions of temperature and pres sure employed and the purity of the product desired. In general, the temperature conditions described in the examples have given good results for the specific fluorination reactions involved. For the production of difiuoro-dichloro methane from carbon tetrachloride, temperatures below about C. are preferably used in this step.

It is recognized that the compositions of the scrubbing liquids after the operation is under way are not the same as those of the original liquids.

Also, the compositions of the scrubbing liquids vary with temperature.

The exact method of procedure used in practising the invention may vary widely. In general, it has been found desirable to treat the reaction gases with the heated scrubbing liquid first and then the cooler scrubbing liquid. Instead of two'scrubblng liquids, a succession of a larger number of baths may be placed in series; the temperature of each bath being so regulated that it is lower than the temperature of the preceding bath. According to this method of procedure, substantially all of the unconverted organic raw materials and a very high proportion of the partially fiuorinated compounds present in the reaction gases, as well as volatilized catalyst, may be removed prior to further purifying, condensing and finally distilling the product.

The invention provides a valuable improvement in processes for the production of fiuorinated acyclic hydrocarbons of the character described. The efficient removal of the antimonycatalyst from the reaction gases and its return to the reaction vessel not only represents a considerable economic benefit-but also greatly facilitates the operation of the process in the prevention of antimony plugs in various portions of the system.

Throughout the specification and claims, it will be understood that by the expression incompletely fiuorinated it is intended to include unconverted acyclic halogen compounds containing no fiuorine as well as partially fiuorinated compounds.

As many apparently widely difierent embodiments of this invention may be made without departing from the spirit and scope thereof, it is to be understood that we do not limit ourselves to the specific embodiments thereof except as defined in the following claims.

We claim:

1. In a process of producing organic fluorine compounds involving a fluorination in the presence of a volatile antimony fluorinating catalyst and removal from the reaction zone of evolved vapors containing fiuorinated compounds and volatilized catalyst as well as other substances, the step which comprises passing the evolved vapors through at least two scrubbing baths in series of a halogenated acyclic hydrocarbon, the temperature of each bath being lower than that of the preceding one.

2. In a process of producing organic fluorine compounds involving a fluorination in the presence of a volatile antimony halide and removal from the reaction zone of evolved vapors containing fiuorinated compounds and volatilized antimony halide as well as other substances, the step which comprises passing the evolved vapors through at least two scrubbing baths in series of a halogenated acyclic hydrocarbon, the temperature of each bath being lower,than that of the preceding one.

3.v In a. process of producing fiuorinated acyclic bath containing a, halogenated acyclic hydrocarbon which is the same as that being fiuorinated, subsequently passing the'resultant gases through at least one other scrubbing bath or the halogenated acyclic hydrocarbon raw material maintalned at a lower temperature than the preceding bath and at a temperature sufiiciently low to .condense incompletely fiuorinated compounds,

-and introducing the scrubbing baths into the;

fluorination reaction zone.

4. The process of claim 1 in which the material contained in the scrubbing baths is introduced into the reaction zone. I

5. The process 01' claim 2 in which the material contained in the scrubbing baths is introduced into the reaction zone.

6. The process of claim 3 in-which the halogenated acyclic hydrocarbon raw material is carbon tetrachloride. p

7. In a process of producing difluoro-dichloro methane involving fluorination of carbon tetrachloride with substantially anhydrous hydrogen fluoride in the presence of an antimony fluorochloride, the step which comprises passing the vapors evolved from the reaction zone through a bath containing principally carbon tetrachloride maintained at a temperature of about 30 C. to about C., then passing the resultant vapors through a second bath containing principally carbon tetrachloride and fluoro-trichloro methane maintained at a temperature below about 0 C., and introducing said baths into the fiuorination reaction zone. v

8. In a process of producing fiuorinated acyclic hydrocarbons involving fluorination of a halogenated acyclic hydrocarbon containing at least one halogen atom other than fluorine in the presence of an antimony halide and removal from the reaction zone oi evolved vapors containing fluorihated compounds and volatilized atimony halide,

the step which comprises passing the evolved vapors through a liquid halogenated acyclic hydrocarbon heated substantially above room temperature.

9. In a process of producing fluorinated acyclic hydrocarbons involving fiuorination of a halogenated acyclic hydrocarbon containing at least one halogen atom other than fluorine in the presence 01' anantimony halide and removal from the reaction zone oi evolved vapors containing fluorinated compounds and volatilizedantimony halide,

the step which comprises passing the evolved vapors through a liquid halogenated acyclic hydrocarbon heated substantially above room temperature under superatmospheric pressure.

10. In. a process of producing fluorinated ethanes involving fiuorination oi perchloroethylene with substantially anhydrous hydrogen fluoride in the presence of an antimony fluorochloride, the step which comprises passing the vapors evolved from the reaction zone through a bath containing principally perchloroethylene maintained at a temperature of about to about C.

11. In a process of producing fluorinated ethanes involving fluorination of perchloroethylene with substantially anhydrous hydrogen fluoride in the presence of an antimony fluorochloride, the step which comprises passing the vapors evolved from the reaction zone through a bath containing principally perchloroethylene maintained at a temperature of about 90 to about 100 C. under superatmospheric pressure.

HERBERT WILKENS DAUDT. MORTIMER. ALEXANDER YOUKER. 

